CN103415475A - Biological wastewater treatment and reuse by utilizing sulfur compounds as electron carrier to minimize sludge production - Google Patents

Abstract

Provided is a method of biological wastewater treatment of influent containing organic carbon, which is performed by oxidizing organic carbon with sulfur or a sulfur compound as an electron carrier, and reducing the sulfur or sulfur compound to sulfide. The sulfide is oxidized with nitrate or oxygen. If necessary, ammonia is oxidized to nitrate and then reduced to nitrogen gas. Also provided is a biological wastewater treatment plant. The method is effective for saline wastewater facilities, as well as non-saline wastewater facilities.

Description

Using sulphur compound as electron carrier to realize the minimized biological sewage treatment of sludge yield and reuse

Background technology

In 20 beginnings of the century, the discharge of organic pollutant makes water pollute has become a main worldwide environmental problem, arises at the historic moment as the biological de-carbon technique of second-stage treatment.Although public health investigator has thereafter transferred to focus development biological removal nutrition technique and has solved eutrophication problem, and there are many competent authoritys also to formulate criterion and standard is controlled sensitive water body nitrogen phosphorus emission, but can not therefore ignore the advantage of second-stage treatment.These advantages comprise shorter mud age, less reactor, easier operation and bubble problem still less.

Environmental Protection Agency (USEPA) definition second-stage treatment in 1984 is the carbon biochemical oxygen demand (BOD) (CBOD of average water outlet in 30 days ₅) and suspended solids (SS) respectively not higher than 25mg/L and 30mg/L.These operations and economically advantage make second-stage treatment remain a kind of of most popular in the world water technology, and the more insensitive water body and the sewage that particularly for water outlet, directly are discharged into as sea are recycled into reuse water.

Reuse water is one of common application of secondary treatment yielding water for irrigating.Irrigation water accounts for 70% of World Water consumption.In order to save valuable water resources, many cities all adopt double water system supply fresh water and reuse water to meet different demands, such as crops is irrigated and the view irrigation.Irrigating desired minimum processing horizontal is exactly that second-stage treatment adds sterilization.Based on the purpose of irrigating, second-stage treatment is better than the biological nutrition material and removes.Not only low because of processing cost, and can retain the nutrient as fertilizer sources.

Since 1914, introduce activated sludge process, with second-stage treatment, remove the biological respinse program in organic carbon technique in sewage and almost do not become.Fig. 1 is exactly one and describes the process flow sheet how the traditional biological sewage treatment process utilizes heterotrophism oxidation reactor removal organic carbon.Treating processes comprises that heterotrophism oxidation organic carbon becomes CO ₂And will remain organic carbon and be converted into mud and removed at second pond.

In order to control eutrophication, to denitrogenate, be necessary.The biological removal of nitrogen technique that generation nineteen sixty grows up is revised treatment process by introducing Autotrophic nitrification and heterotrophic denitrification step.Fig. 2 is a kind of traditional biological processing technological flow figure that a description application heterotrophic denitrification and Autotrophic nitrification reactor are removed carbon, nitrogen.Because the sludge yield coefficients comparison of heterotrophism oxidation of coal and heterotrophic denitrification process is high, in treating processes, the eliminating of excess sludge, processing and disposal are inevitable.

During many countries relied on, the water reuse provided dissimilar reuse water, such as cleaning street and automobile, flush the toilet, view irrigation, wateruse for environment and groundwater recharge.Fig. 3 has showed a typical sewage disposal and has reclaimed the treatment scheme of factory.As a rule, the minimum processing requirements of the reuse water of these types comprises the two stage biological processing and closelys follow sand filtration or membrane filtration and sterilization thereafter.Can increase again denitrogenation, i.e. nitration denitrification technique if necessary.

Yet, at some, utilize area (such as Hong Kong) the application waste water reuse system meeting difficult of seawater toilet-flushing for saving water.This is because the about 35000mg/L of seawater saliferous, when utilizing it to flush the toilet, will form the waste water of saltiness 7000-10000mg/L.So high saltiness can directly have influence on waste water recycling, such as irrigation or recharge of groundwater etc.Yet, due to seawater, also containing simultaneously the vitriol of the 2600mg/L that has an appointment, it can provide enough sulfate ions to form a kind of Novel waste water technology as electron carrier.This feature of the technique of vitriol for SANI technique of utilizing.

Summary of the invention

By utilizing sulphur or sulphur compound, as electron carrier, organic carbon is oxidized into to carbonic acid gas, and described sulphur or sulphur compound are reduced to sulfide, thereby realization contains the biological treatment of the water inlet of organic carbon.This sulfide can be by oxygen or nitrate oxidation afterwards, if by the nitrate oxidation, nitrate will be reduced into nitrogen.

The accompanying drawing explanation

Fig. 1 (prior art) is the traditional biological sewage treatment process figure that utilizes heterotrophism oxidation reactor de-carbon.

Fig. 2 (prior art) is a kind of traditional biological processing technological flow figure that application heterotrophic denitrification and Autotrophic nitrification reactor are removed carbon

Fig. 3 has showed typical sewage disposal and has reclaimed the treatment scheme of factory.

Fig. 4 is the schema of sulfate reduction, autotrophic denitrification, nitrated integrated treatment process (SANI).

Fig. 5 has described the process of three circulation SANI techniques.

Fig. 6 is the biological respinse statement of sulphur compound oxidation.

Fig. 7 is the process flow sheet of the SANI technique of having described revision (simplifying version SANI technique).

Fig. 8 has described sulphur reduction granular sludge bed reactor.

Fig. 9 has described heterotrophism oxidation SANI technique.

Figure 10 has described the heterotrophism oxidation SANI technique of simplifying version.

Figure 11 has described the heterotrophism oxidation SANI technique of extending version.

Figure 12 has described the possible revision of heterotrophism oxidation SANI technique.

Figure 13 has described the design of SANI technique pilot scale structures.

Figure 14 has showed the design of simplifying version SANI technique.

Figure 15 is the chart of showing chemical oxygen demand (COD) (COD) and COD clearance in the water inlet of upflowing sulphur reduction granular sludge bed reactor, water outlet.

Figure 16 a is one group of Photomicrograph of describing sulfate reduction granule sludge form to d.A is the granular sludge state of the 30th day; B observes the photo of granular sludge in the 30th day with the X-ray diffraction; C is the granular sludge form of the 60th day, and d is the granular sludge form of 90 days.

Figure 17 a and b are the charts of describing five minutes sludge volume indexes (SVI5) of domestication and mud granule size.

Figure 18 a and b have described the treatment effect of autotrophic denitrification reactor.A has explained Inlet and outlet water nitrate concentration and nitrate removal rate; B has explained the total organic carbon (TOC) of Inlet and outlet water.

Figure 19 is a Photomicrograph of showing the 65th day mud granule form of autotrophic denitrification reactor.

Figure 20 has described the size distribution of mud granule in the autotrophic denitrification reactor.

Figure 21 has showed that traditional biological denitrogenates the operational scheme with middle water reuse facility.

Figure 22 has showed complete heterotrophism oxidation SANI technique.

Figure 23 has described and has simplified version heterotrophism oxidation SANI technique.

Embodiment

Fig. 4 is the schema of sulfate reduction, autotrophic denitrification, nitrated integrated treatment process (SANI technique).SANI technique is incorporated into carbon and nitrogen cycle by sulphur reduction and oxidation, can effectively minimize the sludge yield of biological waste water treatment processes like this.

Seawater contains the salt of 2600mg/L vitriol and 35000mg/L.Different with the place that utilizes fresh water to flush the toilet in the world, seawater toilet-flushing is used in Hong Kong for water saving.Seawater toilet-flushing can make sewage contain about 600mg/L vitriol and about 7000-10000mg/L salt, compares and accounts for 20-30% with seawater (35000mg/L).The technology disclosed is by utilizing relevant sulfate ion to realize effectively processing this brine waste.Processing non-brine waste can be by introducing the vitriol in seawater or trade effluent, and then to utilize this gate technique to process be also effective.

According to the most original configuration, SANI technique is exactly to rely on as electron carrier, to realize bio-oxidation de-carbon purpose from the vitriol of salt water flushing system.Vitriol in this technology utilization seawater and sulphate reducing bacteria are realized organic carbon is oxidized to carbonic acid gas and autotrophic denitrification and sulfide is changed into to sulfate radical again.Correspondingly, the removal of carbon and nitrogen all needs to depend on the vitriol provided by seawater to change into sulfide.

What the present invention disclosed is the technique about improved sulfate reduction, autotrophic denitrification, nitrated integrated (SANI).Still with reference to figure 4, in SANI technique, the vitriol from seawater in first reactor can be oxidized to carbonic acid gas by organic carbon, and vitriol is reduced to solvability sulfide by sulphate reducing bacteria simultaneously.On the other hand, ammonia-state nitrogen is oxidized by oxygen as nitrate in the 3rd reactor, then this nitrate is back to second reactor and sulfide reacts, this process nitrate will by the autotrophic denitrification bacterial reduction be nitrogen simultaneously sulfide be converted to vitriol.These three main Biochemical processes all produce minimum mud, and reaction process is as shown in following equation:

The heterotrophism sulfate reduction:

$100\mathrm{gCOD}+150.2\mathrm{<figure-callout\; id="4"\; label="g\; SO"\; filenames="HDA00003282823700072.png,HDA00003282823700082.png"\; state="\{\{state\}\}">g</figure-callout>}{\mathrm{SO}}_{}^{}{}_4^{2-}+43.7g{H}_{2}O\&RightArrow;53.2g{H}_{2}S+1.9\mathrm{gSludge}+190.9\mathrm{gHC}{O}_3^{-}$

Equation 1

The oxidation of autotrophy sulfide and denitrification:

$10\mathrm{gN}{O}_3^{-}+0.59\mathrm{gHC}{O}_3^{-}+3.59g{H}_{2}S\&RightArrow;2.26\mathrm{<figure-callout\; id="2"\; label="g\; N"\; filenames="DEST\_PATH\_HDA0000374829060000015.png,HDA00003282823700051.png"\; state="\{\{state\}\}">g</figure-callout>}{N}_{}{}_2+10.14\mathrm{<figure-callout\; id="4"\; label="gS\; O"\; filenames="HDA00003282823700072.png,HDA00003282823700082.png"\; state="\{\{state\}\}">gS</figure-callout>}{O}_{}^{}{}_4^{2-}+0.22\mathrm{gSludge}$

Equation 2

Autotrophic nitrification:

$10\mathrm{<figure-callout\; id="4"\; label="gN\; H"\; filenames="HDA00003282823700072.png,HDA00003282823700082.png"\; state="\{\{state\}\}">gN</figure-callout>}{H}_{}^{}{}_4^{+}+0.73\mathrm{<figure-callout\; id="2"\; label="g\; CO"\; filenames="DEST\_PATH\_HDA0000374829060000015.png,HDA00003282823700051.png"\; state="\{\{state\}\}">g</figure-callout>}{\mathrm{CO}}_{}{}_2+34.67\mathrm{<figure-callout\; id="2"\; label="g\; O"\; filenames="DEST\_PATH\_HDA0000374829060000015.png,HDA00003282823700051.png"\; state="\{\{state\}\}">g</figure-callout>}{O}_{}{}_2\&RightArrow;0.52\mathrm{gSludge}+34.44\mathrm{gN}{O}_3^{-}+1.11g{H}^{+}+9.8g{H}_{2}O$

Equation 3

Fig. 5 is three circulation SANI process flow sheets.Because seawater or vitriol often do not have, therefore the technology modification SANI technique of the present invention's disclosure is three circulation SANI techniques, it can utilize other sulphur compound to comprise that sulphite, thiosulphate or elemental sulfur are as electron carrier like this, with by the reduction of heterotrophism sulphur, autotrophic denitrification and Autotrophic nitrification by electronics by Organic Carbon Transfer to oxygen.In three circulation SANI techniques, sulphite, thiosulphate and elemental sulfur oxidation and reduction circulation are introduced in carbon, nitrogen cycle.These sulphur compounds be used as electron carrier with by the reduction of heterotrophism sulphur, autotrophic denitrification and Autotrophic nitrification by electronics by Organic Carbon Transfer to oxygen.

As shown in Figure 5, three circulation SANI techniques comprise following bioprocess:

In first reactor, electronics by sulphate reducing bacteria by Organic Carbon Transfer to sulphur.By the reduction of heterotrophism sulphur, sulphur compound is reduced into sulfide while organic carbon and is oxidized to carbonic acid gas, and the sulfide of formation will enter second reactor subsequently.

In second reactor, electronics is transferred to nitrate by autotrophy sulphur oxidation/denitrifying bacterium by sulfide.By autotrophic denitrification, sulfide is oxidized to vitriol while nitrate and is reduced into nitrogen.

In the 3rd reactor, electronics is transferred to oxygen by the Autotrophic nitrification bacterium by ammonia.By the Autotrophic nitrification ammonia, will be oxidized to nitrate, then be back to second reactor and participate in the autotrophic denitrification process.

By three circulation SANI techniques, not only can utilize vitriol, and can utilize sulphite, thiosulphate or elemental sulfur to realize that biological removal of nitrogen and sludge yield minimize.

This process makes full use the oxidation of multivalence state sulphur and reduction and the autotrophic denitrification that reduction process completes sulphur.Fig. 6 and equation 4 are illustrated in the main sulfur oxidizing organism metabolic process in autotrophic denitrification.And the reversal procedures in these reactions, i.e. the reduction of the sulphur compound after oxidation, completed by the sulphur reducing bacteria.According to reactor design, determine, three circulation SANI techniques can utilize various bio-reactor to carry out, for example separation sludge system, sequencing batch reactor, membrane bioreactor, upflow sludge blanket system or the moving-burden bed reactor of Sludge System, utilization contact growth bacteria bed.

$10\mathrm{gN}{O}_3^{-}+0.59\mathrm{gHC}{O}_3^{-}+3.59g{H}_{2}S\&RightArrow;2.26\mathrm{<figure-callout\; id="2"\; label="g\; N"\; filenames="DEST\_PATH\_HDA0000374829060000015.png,HDA00003282823700051.png"\; state="\{\{state\}\}">g</figure-callout>}{N}_{}{}_2+10.14\mathrm{<figure-callout\; id="4"\; label="gS\; O"\; filenames="HDA00003282823700072.png,HDA00003282823700082.png"\; state="\{\{state\}\}">gS</figure-callout>}{O}_{}^{}{}_4^{2-}+0.22\mathrm{gSludge}$

Equation 4

The biologic treating technique that other has disclosed, be mainly the reduction of heterotrophism sulphur, autotrophic denitrification and Autotrophic nitrification, all has very low mud production rate coefficient.The biosolids refuse that three circulation SANI techniques produce is few, can save the sludge disposal expense in actual applications, saves and is equivalent to 50% of cost of sewage disposal, can reduce approximately 1/3 energy consumption and greenhouse gas emission simultaneously.

Fig. 4 and Fig. 5 show the contrast of original SANI technique and three circulation SANI techniques.Shown in its name, original SANI technique (Fig. 4) is to rely on sulfate ion as electron carrier.With original SANI technique, compare, three circulation SANI techniques (Fig. 5) can utilize the sulphur compound of various valence states to comprise that vitriol, sulphite, thiosulphate and elemental sulfur complete the removal of carbon, nitrogen as electron carrier.The application that original SANI has been expanded in this development greatly, can be used to from other De Liu source, various wastewater source, such as the waste water of incinerator flue gas desulfurization it.

Three circulation SANI techniques of a revision are not requiring in the occasion of denitrogenation it is very useful.Fig. 7 is exactly the schema that is called as the revision SANI technique of simplifying version SANI technique.As above said, because denitrogenation is always not necessary, therefore developed a SANI technique of simplifying version.Simplifying in version SANI technique, the sulphur oxidation reduction cycle combines with the oxidation of coal circulation.With three circulation SANI resemble process, by sulphur, reduce and the oxidation of autotrophy sulphur, the sulphur compound of different valence state is such as vitriol, sulphite, thiosulphate and elemental sulfur can be used as electron carrier, so that electronics is delivered to oxygen from organic carbon.Simplify version SANI technique and can be used as biological de-carbon or second-stage treatment, simultaneously can be so that sludge yield minimizes.

As shown in figure seven, in first reactor, electronics flows to sulphur by the sulphur reducing bacteria by organic carbon, and sulphur compound can be reduced into sulfide while organic carbon and be oxidized to carbonic acid gas, and the sulfide of generation enters second reactor subsequently.Electronics flows to oxygen by the autotrophy sulfur-oxidizing bacteria simultaneously sulfide is oxidized there.

With SANI technique, compare, simplifying version SANI technique does not need the denitrogenation part.Although there is no denitrification reactor, remove if necessary poisonous ammonia, the SANI technique of simplifying version also can provide Autotrophic nitrification that ammonia is changed into to nitrate in the second reactor.

Design and the electronics of simplifying version SANI flow by following bioprocess realization:

At first reactor, electronics flows to sulphur from organic carbon.By the reduction of heterotrophism sulphur, sulphur compound is reduced into sulfide while organic carbon and is oxidized to carbonic acid gas, and the sulfide of formation enters into second reactor subsequently.

In second reactor, by autotrophy sulphur oxidising process, electronics flows to oxygen from sulfide, and sulfide is oxidized simultaneously.

Fig. 1 and Fig. 7 show traditional waste water treatment process and simplify the contrast of version SANI technique.With traditional second-stage treatment technology, compare, simplify version SANI introducing sulphur cycle and realize the organic carbon oxidation.Although simplifying version SANI technique and original SANI technique is all to utilize heterotrophism sulphur also originally organic carbon to be oxidized to carbonic acid gas, the oxidation of sulfide is but two complete different paths.With original SANI technique, compare the nitrogen cycle part of having simplified version SANI technique economization.In original SANI technique, the oxidation of sulfide realizes by autotrophic denitrification, and from sulfide, to flow to nitrate be nitrogen by nitrate transformation to electronics simultaneously in this process, and make electronics directly flow to oxygen by Autotrophic nitrification.Simplifying in version SANI technique, the oxidation of sulfide is by autotrophy sulfide oxidising process directly by dioxygen oxidation, and electronics is directly transferred to oxygen from sulfide in this process, not through peroxy-nitrate.

Further revising the three circulation SANI techniques of advising can provide the granular sludge bed reactor of sulphur reduction and the oxidation of autotrophy sulfide.

Just as all biological wastewater treatment processes, the efficiency of three circulation SANI techniques and simplification version SANI technique all highly depends on the microorganism concn in reactor.For efficiency and the validity that improves reactor, upflow type anaerobic sulfate reduction granular sludge bed reactor and upflowing autotrophic denitrification granular sludge bed reactor have been developed.These two reactors are the usefulness of accelerating whole treating processes.

Fig. 8 is the schematic diagram of sulphur reduction granular sludge bed reactor.Organic carbon is oxidized to carbonic acid gas while sulphur compound and is reduced into sulfide in this reactor.As shown in the reaction of Fig. 6, due to vitriol, be the highest oxidation state of sulphur reduction process, so this reactor is equally applicable to reduce other valence state sulphur compound, as sulphite, thiosulphate and elemental sulfur etc.

By in reactor, maintaining high upflow velocity and keeping artificial turbulent flow fully to stir and to mix, the mud in reactor can form high density granular like this.Because the concentration of granule sludge will be far above traditional complete, so apply the granular mud bed volume that can obviously reduce treatment facility.

Although the granular sledge bed bioreactor has been applied on other sewage treatment process, this granular sledge bed bioreactor is diverse with other granular sledge bed system.Significantly be not both: the bioprocess (i) related to is fully different; The microorganism (ii) related to is fully different; (iii) at sulfate-reducing process, there is no γ-ray emission, yet other granular sledge bed bioreactor all involves stirring and the mixing of gas.These differences are specific as follows:

What up-flow anaerobic sludge blanket (UASB) reactor carried out is anaerobic fermentation process.In the UASB reactor, important reaction process is to produce methane gas by anaerobically fermenting.These organic substances can pass through unbecoming chemical reaction.And the bacterium that participates in reaction is mainly zymophyte and methanogen.In this reactor, washing away of the mixing of waste water and mud mainly depends on the stirring brought by forming of methane gas.

Anaerobic degradation process: C ₆H ₁₂O ₆→ 3CH _{4 (g)}+ 3CO2

Equation 5

The granulating activated sludge reactor can the oxidation organic carbon.In reactor by adding air to realize the oxidation of organic carbon.This bioprocess is completed by heterotrophism oxidation of coal bacterium.By adding air for system provides a powerful stirring, system is mixed and wash away fully simultaneously mud.

Aerobic degradation: C ₆H ₁₂O _{6 (aq)}+ 6O _{2 (g)}→ 6CO _{2 (g)}+ 6H ₂O _(l)

Equation 6

What the particle anaerobic ammonia oxidation reactor carried out is that reaction process produces a large amount of nitrogen by the leading reaction of anaerobic ammonium oxidizing bacteria, makes muddy water in reactor fully stir mixing, washes away simultaneously the mud of the inside.

Anammox reaction: NO ₂ ^- _(aq)+ NH _{3 (aq)}+ H ⁺ _(aq)→ N _{2 (g)}+ 2H ₂O _(l)

Equation 7

Sulphur reduction granular sludge bed reactor is mainly used in the organic carbon oxidation.The oxidation of organic carbon is to realize by sulphur reducing bacteria and the sulphur compound added.Because reaction relates to, strong acid (vitriol) is changed into to weak acid (sulfide), so after reaction, the pH value of system can improve, thereby make carbonic acid gas and sulfide all dissolve fully.Therefore whole reaction does not involve gas phase, and the mixing of system is controlled by liquid phase fully.And, because the growth velocity of sulfate-reducing bacteria is very low, compare with aerobic sludge method or fermenting process, do not need continuous spoil disposal.

Sulfate-reducing process: C ₆H ₁₂O _{6 (aq)}+ 3SO ₄ ^2- _(aq)→ 6CO _{2 (aq)}+ 6H ₂O _(l)+ 3S ^2- _(aq)

Equation 8

Sulfate reduction does not involve any gas-phase reaction, unlike aerobic oxidation and anaerobism methane-producing reactor, relies on the gas produced and makes reactor mix.Therefore, the sulphur reduction reactor only relies on liquid-flow mixes muddy water, provides simultaneously necessary turbulent flow to wash away mud to form granule sludge.And, owing to there is no gas phase, there is no need as anaerobism is produced methane granule sludge bed system a three-phase (being gas/liquid/solid) separator to be set.

When streaming sulphur reduces granular sludge bed reactor in design, introduced two specific functions, comprised and use recycle pump to manufacture the turbulent flow in reactor with the section upflow velocity and the use traffic limiting device that improve in reactor.

In experimental reactor, can use a trilateral baffle plate to equip as flow restriction around reactor.Introducing this two large specific function can bring up to the upflow velocity at baffle plate place into five times of the water flow velocity, can obviously strengthen like this mud motion in reactor.Except bringing necessary mixing for sewage chemical oxygen demand (COD), sulfate ion and mud, this two large specific function can also wash away loosely organized mud, form a shearing force, thus the growth of reinforcement sludge, so that mud is to closely abundant granule sludge development.

Similar with sulphur reduction granular sludge bed reactor, the efficiency of autotrophic organism sulfide oxidation particle sludge bed reactor is also biomass concentration and the biomass vigor highly depended in reactor.Upflowing autotrophy sulfide oxidation particle sludge bed reactor is used for achieving this end exactly.In order to improve three circulation SANI techniques and to simplify edition processing efficiency and the validity of SANI technique, developed a upflowing autotrophy sulfide oxidation particle sludge bed reactor.This upflowing autotrophy sulfide oxidation particle sludge bed reactor has used identical design to promote the usefulness of whole reactor.This reactor can be by following two mechanism to realize the oxidation of autotrophy sulfide: (a) as shown in equation 9, using oxygen as electron acceptor(EA), and (b) as shown in equation 10, using nitrate as electron acceptor(EA).Owing to having produced nitrogen, when being necessary, can add at the top of reactor a three-phase (, gas-liquid-solid) separator.

Although granular sludge bed reactor has been applied in other wastewater treatment process, this treatment process process and other granule sludge bed system are different, mainly as follows: the bioprocess (i) related to is fully different; The microorganism (ii) related to is fully different.These differences are specific as follows:

In autotrophy sulfide oxidising process, the biochemical reaction related to is as follows:

When the aerobic air lift supplies:

S ^2-+2O ₂→SO ₄ ^2-

Equation 9

Perhaps

When having nitrate to provide:

5S ^2-+8NO ₃ ^-+4H ₂O→5SO ₄ ^2-+4N ₂+8OH ^-

Equation 10

In traditional treatment process, denitrification or oxidising process are heterotrophism processes, are all namely to using organic carbon as electron donor.The microorganism related to is heterotrophic microorganism, and the carbon source of metabolism is organism.Yet in the autotrophy process, sulfide is as electron donor, carbonic acid gas is as carbon source, and the bacterium involved is autotrophic bacteria.

What three circulation SANI techniques uses through further revising added may be from the sulfate ion of seawater.This improvement technology can be regarded a heterotrophism oxidation SANI technique as.

Except Hong Kong is to use seawater toilet-flushing, most places is still used fresh water to flush the toilet in the world.Owing in sewage, not containing seawater, the waste water saltness of these area discharges is not high.Therefore, their waste water just can recycle in different purposes through traditional second-stage treatment (academicly crying the heterotrophism oxidation) and follow-up filtration, disinfectant program, comprises irrigation and recharge of groundwater etc.

Use not containing sulfate of fresh water is flushed the toilet rather than the place of seawater toilet-flushing produces waste water.Because SANI technique relies on vitriol as electron carrier, therefore be necessary to add sulphur compound and maintain sulphur reduction and oxidising process in influent waste water.Yet add the reuse water after perhaps sulfate ion (mainly by adding seawater) can pollute processing, because can improve like this salinity of water outlet, also can cause water outlet can't be back to use on the aspects such as picture irrigation and recharge of groundwater simultaneously.For fear of the value that affects reclaimed water reuse, can utilize again SANI art breading biological wastewater and realize that sludge yield minimizes simultaneously, develop a revision SANI technique, be called heterotrophism oxidation, sulfate reduction, autotrophic denitrification and nitrated integrated (heterotrophism oxidation SANI technique) technique.

In the application that most of sewage reclaims, the amount of reuse water accounts for into 1/3 of water total amount.For example Fla. is that sewage recycling is the most local in the world, and its sewage reclaims consumption and also only accounts for approximately 43% of total sewage load.Therefore, can utilize the difference of these two amounts that the sewage water inlet is divided into to two tributaries, be that first tributary (accounting for 1/3) does not add sulphur compound, directly adopt the traditional biological facture so that reusing sewage, another tributary (accounting for 2/3 flow) adopts SANI technique to minimize to realize sludge yield by adding sulphur compound (such as seawater).The ratio in two tributaries will minimize and determine according to the demand of sewage recycling and processing cost.

Fig. 9 has showed heterotrophism oxidation SANI technique, and it is that a traditional heterotrophism oxidizing process adds a SANI technique of utilizing outside sulphur source.Due to the recycling rate only account for total sewage water inlet ratio lower than 1/3, it is feasible to process respectively that the sewage of therefore intaking is divided into two tributaries.First tributary (account for flooding velocity 1/3) enters into traditional biological treating processes (as shown in Figures 1 and 2), in the situation that do not add sulphur compound, directly utilize the heterotrophism oxidation of coal to process, then water outlet enters into by pump the needs that reuse water manufactory processes to meet different purposes.Mud from the elementary and second-level settling pond in first tributary is transferred to the another one tributary, and collects remaining waste water (that is, account for total flux 2/3) through the SANI art breading.In this process, can obtain by extracting seawater the sulphur source of SANI technique, and intake to mix with sewage.Seawater is a reliable and cheap sulphur source.Can expend when unique extra-expense is exactly extracting seawater.With the sludge treatment expense of saving, to compare be inappreciable yet these can expend.For some, can't utilize the area of seawater, can utilize trade effluent as the sulphur source, such as acidic mine waste water or petrochemical industry power station flue gas desulfurization waste-water.

Heterotrophism oxidation SANI technique can produce the waste water that not polluted by the sulphur source by the first tributary and make different purposes with recycling, such as irrigating and recharge of groundwater, utilizes simultaneously sulphur cycle to realize that in second tributary sludge yield minimizes.Aspect wastewater treatment, the feature of heterotrophism oxidation SANI technique is as follows:

With the traditional wastewater treatment technology, compare, from the coagulation of heterotrophism oxidising process in the first tributary and the mud of second-stage treatment, in the sulfate reduction device, digestion occurs, rather than digest or incinerate by methane-producing reactor.

With SANI technique, compare, three Main changes arranged:

(1) SANI technique is to design to be used for directly processing waste water, and heterotrophism oxidation SANI technique also is used for processing one-level, secondary mud;

(2) the SANI technology utilization is from the vitriol of salt water flushing system, i.e. the sulphur source of water inlet.In heterotrophism oxidation SANI technique, vitriol adds by external source, such as direct extracting seawater.

(3) water outlet of SANI technique also has vitriol and the salinity of high density, has directly limited the reuse of waste water, such as irrigating etc.; Yet heterotrophism oxidation SANI technique can be produced part and be contained the water outlet of low-concentration sulfuric acid salt and salinity in order to recycle in different purposes.

Heterotrophism oxidation SANI technique will be processed waste water and be divided into two tributaries: waste water recycling and water outlet discharge.Can adapt to different Effluent criterias like this.Therefore can require to optimize two large tributary treatment process according to different treatment.Such as in water reuse tributary, saving denitrification process, increase denitrification process in water outlet discharge tributary; Perhaps opposite.

Figure 10 simplifies version heterotrophism oxidation SANI process flow sheet.When draining does not require denitrogenation, can make to simplify the SANI technique in the second tributary into version SANI technique by saving the denitrification step.The design of heterotrophism oxidising process can also further be simplified by the preliminary sedimentation tank of removing the first tributary, as shown in figure 10; Perhaps directly with membrane bioreactor, replace the reactor in the first tributary.

When having need to carry out denitrogenation and require to meet certain for reuse water the time, such as recharge of groundwater, will increase the processing that traditional denitrification process is deepened the first tributary.In addition, also can increase dephosphorization process.Figure 11 is expanding type heterotrophism oxidation SANI process flow sheet.

With traditional biological treatment process, compare, the SANI technique that these are new and design take full advantage of sulphur compound (comprising vitriol, sulphite, thiosulphate and elemental sulfur), as electron carrier, organic carbon are oxidized to carbonic acid gas.Because sulphur reduction and autotrophy sulphur oxidising process have very low sludge yield coefficient, the mud production rate of SANI process is more much lower than traditional biological facture, therefore can effectively minimize sludge yield, thereby exempts follow-up sludge treatment and disposal requirement.

The 40%-60% that mud is concentrated, digestion, dehydration and disposal facility probably account for whole sewage work capital cost, and overall running cost 50%.Because SANI technique can effectively be exempted sludge treatment and disposal, it can save total expenses approximately 50%.And due to sludge dewatering with burn to be consume the energy, therefore with the traditional biological denitrification process, compare, estimate to adopt SANI technique and remove sludge treatment from and burning process can be saved 1/3 the energy and reduce by 1/3 greenhouse gas emission.

Three circulation SANI techniques, simplification version SANI technique and heterotrophism oxidation SANI technique are all emerging biologic treating techniques, they can be applied in different reactor design, such as active sludge, membrane bioreactor, sequencing batch reactor, tower biological filter, aerobic biofilter or moving-bed bioreactor.

In addition, because SANI technique can be processed and compare with traditional biological with comprising that upflowing sulphur reduction granular sludge bed reactor and upflowing sulphur oxidation particle sludge bed reactor or aerobic filter tank carry out sulfur oxide, it can exempt preliminary sedimentation tank and second pond.Yet the disadvantage of removing preliminary sedimentation tank is the hydraulic detention time that may extend whole SANI process.

The advantage of three circulation SANI techniques

The application that three circulation SANI techniques have been expanded original SANI technique, make it not only can utilize vitriol, can also utilize sulphite, thiosulphate and elemental sulfur as electron carrier.This makes the application of SANI technique more flexible, so that also can apply away from the people in sea.Such as the sulphite in the water outlet of incinerator smoke desulfurization is just very abundant, the by product elemental sulfur of a lot of industry is also inexpensive, can be used as the electron carrier of SANI technique.

If do not need denitrogenation, can be by the SANI technology generations of simplifying version for SANI technique.With SANI technique, compare, simplify the SANI technique of version and economize except the anoxic bio-reactor, and the autotrophic denitrification bacterium utilizes sulfide, as electron donor, nitrate reduction is become to nitrogen in this reactor.Therefore effectively so just can reduce by 1/4 total reactor quantity, reduce approximately working cost and the reaction compartment of 25% SANI technique.

With traditional second-stage treatment, compare, the simplification version SANI technique of arranging at present comprises sulfate reduction upflow sludge blanket (SRUSB) and aerobic biofilter (AF), can save preliminary sedimentation tank and second pond.In addition, simplify version SANI technique and can exempt sludge treatment and disposal, can save like this 50% expense.Simplify the reactor that version SANI technique can also be applied to other, such as active sludge, sequencing batch reactor, tower biological filter, aerobic biofilter, membrane bioreactor or moving-bed bioreactor etc.

Sulphur reduction granular sludge bed reactor and autotrophy sulfide oxidation particle sludge bed reactor benefit for improving treatment efficiency.The efficiency height of system depends on the biomass concentration in reactor.The advantage of granular sludge bed reactor can improve reaction efficiency exactly, therefore can save and process space.With traditional suspension growth reactor or flocculation sludge bed reactor, compare, granular sludge bed reactor has higher sludge concentration.Therefore the efficiency of reactor improve greatly, makes hydraulic detention time greatly reduce, and so only needs very little reaction compartment just enough.

Because granule sludge has more outstanding settling property, more easily with go out aqueous phase separation, make water outlet limpider than flocculation Sludge Bed system or suspension growth system.So perhaps, can be without second pond.In addition, because granule sludge is abundant firm, they can resist larger water impact load.

A major advantage of heterotrophism oxidation SANI technique is to utilize SANI technique to realize the minimized while of sludge yield, can also maintain a tributary and use (such as irrigation, recharge of groundwater) on different purposes to produce unpolluted reuse water.As above carry, utilize SANI technique can reduce 1/3 energy consumption and 1/3 greenhouse gas emission.Unique extra-expense is exactly the energy consumption of the seawater of extraction.Yet this compares with the expense of saving sludge treatment and disposal is inappreciable.

Another advantage of heterotrophism oxidation SANI technique is to select different processing to carry out optimization process according to different requirements.A lot of application, such as rinsing street and automobile, flushing the toilet and irrigate, are not need denitrogenation.In fact, nitrogen is retained in reuse water be used for irrigating for plant and benefits.On the other hand, grow thickly for avoiding receiving body eutrophication and algae, the water outlet of discharge needs denitrogenation.These two requirements are sometimes contradiction, and common way is to adopt the treatment technology of high requirement, but can increase working cost like this.

In heterotrophism oxidation SANI technique, the first tributary can adopt biological de-carbon rather than denitrogenation to provide reuse water with for irrigating.Denitrogenation can be put in the SANI technique in the second tributary.It is this that to be arranged in traditional heterotrophism oxidation processes be very difficult sometimes, unless extra carbon source is arranged, such as adding methyl alcohol.This is because traditional denitrification process is being that organic carbon source in waste water is controlled on biodynamics.

On the other hand, the denitrification in SANI technique is an autotrophy process.It does not need carbon source.Therefore the denitrification potential of SANI technique is the twice of traditional biological denitrification process.Heterotrophism oxidation SANI technique does not need additionally to add carbon source also can realize denitrification completely.Figure 12 has showed other possibility revision of heterotrophism oxidation SANI technique.By reducing denitrogenation unit and the preliminary sedimentation tank in the first tributary, can greatly reduce processing space and the running cost in the first tributary, do not increase simultaneously processing space and the running cost in the second tributary.When the slump in demand of reuse water, the autotrophic denitrification reactor that in the first tributary, remaining processing waste water can be drawn into the second tributary carries out denitrogenation.By such layout, not only reaction compartment and processing cost can be minimized, and nutrition can be retained with for irrigating.

By above technology, not only can be by the application of SANI technique to the coastland that does not utilize seawater toilet-flushing, and the requirement that can provide wider selection space to meet discharge water and reuse water, and optimize the process of SANI technique.

Example 1-tri-circulation SANI techniques

In order to confirm the treatment effect of vitriol/sulfide/vitriol circulation, at Xiang Gangdong, gush sewage pumping station and carried out the SANI pilot scale, be used for processing near airport and 83, the sewage that the 000Ren De community is collected.The pilot scale facility comprises upflowing sulfate reduction Sludge Bed (SRUSB) reactor and two upflowings are aerobic and anoxic biological filter (AF) reactor.SRUSB is the anaerobic reactor of a stopping property, diameter 1.6m, high 4.2m, effective volume 6.8m ³.AF has filled plastic carrier (specific surface area 115m ²/ m ³), diameter 1.6m, high 4.4m, effective volume 3.9m ³.SRUSB and AF inoculate from anaerobic digester (MLSS8000mg/L) and the activity sludge reflux section (MLSS4000mg/L) of a local secondary saline sewage treatment plant respectively.

SANI pilot test system continuous water inlet every day 10m ³Carry out.Sewage draws up the first children of process 6mm to sieve filtration from hold well, is not then passing through other primary treatment again, just through intake pump, flows into the SANI pilot test system continuously.Figure 13 is SANI pilot scale schema.Pilot scale design and running parameter such as table one:

Table one pilot scale water factory design and operation parameter

By 24 hours combined sewage samples of periodic analysis, determine the water inlet composition, sum up as table two.By testing, determine in the water inlet organic composition have 8.0% to be voltaile fatty acid (VFA), 21.5% is biodegradable dissolved organic matter, 7.1% is not biodegradable dissolved organic matter, and 50.5% is biodegradable particle state organism, and 12.9% is not biodegradable particle state organism.

The average influent quality of table two SANI pilot scale water factory (after young sieving)

As shown in Figure 4, be used to vitriol in seawater as electron carrier, organic carbon is become to carbonic acid gas by three cyclic oxidations.

Pilot test system has been moved 225 days under steady state.Do not pass through elementary precipitation, the influent quality that pilot test system is processed is COD431mg/L, SS280mg/L, and TN87mg/L, effluent quality are COD54mg/L, SS36mg/L, NH ₄-N3.4mg/L, NO ₃-N16.8mg/L.COD and TSS clearance are respectively 87% and 87%.But the clearance of TN only reaches 55%, some reasons are the ratios of very high (26%) that account for due to the not biodegradable organonitrogen of the solvability from industrial source.

Pilot test system has obviously reduced sludge yield.Biomass during whole service in unpromising Controlling System and arranged mud.With the traditional biological facture, compare, pilot test system has realized mud decrement 90%, and has 84% to be inorganic substance in its remaining 10% sludge creation amount.MLVSS/MLSS in SRUSB is stabilized in 0.7, and average sludge volume index (SVI) is permanent in 110ml/g.Owing to not needing primary clarifier and sludge treatment facility, SANI technique can provide Odor con trol solution more cheaply for saline sewage treatment plant.

The operation of example 2-sulphite/sulfide/vitriol circulation

As shown in Figure 5, the sulphite/sulfide in three circulation SANI techniques/vitriol circulation, the sulphite that can be used in the flue gas desulfurization waste-water in incinerator or fuel-burning power plant replaces vitriol as electron carrier.Because example 1 and example 2 treatment systems main is respectively the layout at the sulphur reduction reactor; Therefore example 2 just represents whole system with the sulphur reduction reactor.The diameter of upflowing sulphur reduction granular sludge bed reactor is 8.8cm, high 50cm, cumulative volume 3L, effective volume 2.85L.The reactor waterpower residence time (HRT) is 12h, and the state that internal reflux is 5 times has moved 7 days, continuous three days subsequently this collection of water sampling data.

Stock solution composition such as the table three of synthetic wastewater.Total COD of stock solution is 60000mg/L, COD:N:P=150:17:1.And the sulfate ion in use S-WAT replacement seawater is as electron carrier.

Table three synthetic wastewater dope and micro solution form

The index that needs to measure comprises Inlet and outlet water TOC, TN, pH, basicity and sulphite, and the sulfate radical of water outlet, thiosulphate and sulfide.Average Inlet and outlet water TOC is respectively 120mg/L and 21mg/L, illustrates that the TOC average removal rate can reach 83%.Average water inlet SO ₃ ²-S is 178mg/L, the SO of average water outlet ₃ ^2--S is 14mg/L, S ₂O ₃ ^2--S6mg/L, SO ₄ ^2--S29mg/L, S ^2--S132mg/L, illustrate that the average sulfur balance is 102%.By the COD:TOC in guestimate glucose, be 2.67, experiment COD balance can accomplish approximately 75%.This experiment has absolutely proved that sulphite can be used as electron carrier oxidation organic carbon and simultaneously sulphite changed into to sulfide.

Example 3-simplifies the application of version SANI technique

Simplifying version SANI system experimentation is to utilize the synthetic wastewater of emulation Hong Kong saline sewage composition to carry out.Storing solution composition such as the table three of preparation synthetic wastewater.Total COD of storing solution is 60000mg/L, COD:N:P=150:17:1.Storing solution and seawater (sulfate concentration is 2700mg/L, and chlorine ion concentration is 19000mg/L) mix, and then with tap water, dilute to obtain required COD concentration (400mg/L).

By carbon, sulphur cycle as shown in Figure 7, simplify the oxide sulfate organic carbon in version SANI technology utilization seawater.Except the vitriol from seawater, the sulphur compound of other type also can be used as electron carrier.Such as the vitriol from sucrose waste water or acidic mine waste water and can be as electron carrier from the sulphite of petrochemical industry power station flue gas desulfurization waste-water.

Simplify SANI technological design such as Figure 14 of version.SRUSB reactor inside diameter in test is 5.4cm, height 44cm, cumulative volume 1L.Its hydraulic detention time is 3hr, and internal reflux is 4.Aerobic biofilter (AF) reactor inside diameter 5.4cm, height 32cm, effective volume 400ml.The HRT of aerobic biofilter (AF) reactor is 1.2hr, there is no internal reflux.

The sulfate reduction device is 3.2kg COD/m at organic loading ³Under the condition in/sky, operation can obtain 89.3% average COD removal.The solvability sulfide concentration of water outlet is 114.7mg S ^2--S/L, Inlet and outlet water vitriol differs 128mg SO simultaneously ₄ ^2--S/L, so reactor reaches the sulphur budget to 89.6%.

In autotrophy sulphur oxidation reactor, the sulfide that the sulphur reduction reactor produces will be oxidized to vitriol.Oxidized except sulfide, the ammonia of part water inlet can be by nitrated one-tenth nitrate, and making the water outlet ammonia nitrogen concentration is 15.4mg/L, and nitrate concentration is 25.4mg NO ₃ ^-N/L.

The final outflow water COD that simplifies generally version SANI experimental reactor is 25.2mg/L, and SS is 47.2mg/L, and the COD clearance can reach 93.7%.The UV optical transmittance of final outflow water under wavelength 254nm is 75%.In whole lab investigation, reactor does not have excess sludge to need to get rid of.

In example 4-simplification version SANI technique, try out

This experiment is to utilize the processing water yield that the actual sewage in Hong Kong carries out to reach 10m ³The pilot scale in/sky, experimental results show that simplification version SANI process operation is satisfactory, do not have excess sludge to produce.As shown in figure 14, this is simplified the pilot scale of version SANI technique and gushes sewage pumping station and carry out in (with seawater toilet-flushing) east in Hong Kong, and its experimental design and example 1 are similar.The pilot scale design is comprised of the aerobic biofilter of a upflow type anaerobic sulfate reduction Sludge Bed and the oxidation of an autotrophy sulfide, and whole pilot scale has moved 100 days under steady state conditions.

The layout of the inoculation of design, water inlet and the mud of SRUSB and AF reactor all follows example 1 the same.After the domestication of month, simplify version SANI pilot scale and enter the steady state conditions operation, design parameter such as table four:

SANI pilot scale water factory operational condition under table four stable state

At organic loading, be 0.63kg COD/m ³Under/day condition, SRUSB COD average removal rate under steady state conditions reaches 77.1%, and going out the water-soluble sulfide concentration is 124.1mgS ^2--S/L, Inlet and outlet water sulfate concentration difference is 130.3mg SO simultaneously ₄ ^2--S/L, mean that corresponding sulphur budget can reach 95%.

The sulfide that SRUSB produces can be oxidized to vitriol at AF.Except sulfide was oxidized, the ammonia of part water inlet can be by nitrated one-tenth nitrate, and the concentration that makes water outlet ammonia is 25.8mg NH ₄-N/L, nitrate concentration are 18.8mg NO ₃-N/L.

On the whole, simplifying version SANI technique final outflow water water quality is that COD63.4mg/L and SS are 42.1mg/L, and corresponding COD and SS average removal rate can reach respectively 85% and 85%.Final outflow water is that under 254nm, the UV optical transmittance is 75% at wavelength, illustrates that water outlet can utilize UV to carry out disinfection.In this pilot process, simplifying version SANI technique does not need to discharge excess sludge.

Because heterotrophic organism produces more mud than autotrophic bacteria usually, so the sludge yield analysis mainly concentrates on the SRUSB reactor.The average MLVSS concentration of SRUSB is about 3500mg/L, and the mean ratio of MLVSS/MLSS is 0.7, and sludge volume index (SVI) is lower than 110mL/g.The observed growth yield coefficient of SRUSB is 0.02kg VSS/kg COD, compares with traditional second-stage treatment, has reduced by 90% sludge yield.Confirming does not simultaneously have excess sludge to discharge outward yet.

The operation for the treatment of plant and sludge treatment are the two large sources that consume the energy and discharge carbonic acid gas.According to estimates, simplify version SANI technique owing to not having excess sludge to need discharge, compare and can reduce by 1/3 energy consumption and greenhouse gas emission with traditional second-stage treatment.

The operation of example 5-sulfate reduction granular sludge bed reactor

This experiment has utilized that sulfate reduction as used as example 2 is granular mud bed to carry out.Upflowing sulphur reduction granular sludge bed reactor diameter is 8.8cm, high 50cm, and cumulative volume 3L, effectively utilize volume 2.85L.Figure has showed upflowing sulfate reduction granular sludge reactor Inlet and outlet water COD concentration and clearance.Chart has been showed the upflowing sulfate reduction granule sludge bed operating treatment effect of 130 days.

The about 300-350mg/L of inlet COD concentration, the about 30mg/L of effluent COD concentration.The COD clearance is stabilized in 90% after operation in 80 days, is 1hr even work as hydraulic detention time.Simultaneously most sulfate ion (approximately 70%) is reduced to sulfide.

Figure 16 a is one group of photo of describing sulfate reduction granule sludge form to d.A is the granular sludge state of the 30th day; B observes the photo of granular sludge in the 30th day with the X-ray diffraction; C is the granular sludge form of the 60th day, and d is the granular sludge form of 90 days.Microscopic examination shows that in two months, all mud in reactor are granulating.These particle shapes are spherical in shape and gem-pure profile, approximately 2 millimeters of mean diameters arranged.

Figure 17 a and b are five minutes sludge volume index (SVI that describe domestication ₅) and the mud granule size.Five minutes sludge volume indexes of seed sludge are 80mL/g, and particle diameter is 44 microns.Most of mud becomes flocculence in 15 days that start.Move and start to form granule sludge after 30 days.After domestication, sludge volume index descended gradually in five days, and particle diameter increases, and operation transferred to stable through 60 days operation post-reactors.

Example 6-autotrophy sulfide oxidation particle sludge bed reactor

In order showing, to use granule sludge to realize the advantage of autotrophy sulfide oxidation, to have built autotrophic denitrification (AD) granular sludge bed reactor of an experimental size.This autotrophic denitrification granular sludge bed reactor diameter is 6.2cm, high 33.5cm, and cumulative volume 0.95L, effectively utilize volume 0.85L.The reactor seed sludge picks up from the anaerobic sludge digester of a local brine waste treatment plant.

Two kinds of synthetic wastewaters that contain respectively SODIUMNITRATE 30mg N/L and sodium sulphite 60mg S/L are used in experiment.In service at first 60 days (that is, the stage 1), according to shown in table five, the waste water of two types is all added into to meet required load.During the 61st day to the 130th day (stage 2), then utilize the sulfate reduction granular sludge bed reactor water outlet of example 5 to replace synthesizing sulfide waste water.

Table five autotrophic denitrification reactor operating condition

Figure 18 a and b describe the treatment effect of autotrophic denitrification reactor.Figure 18 a has showed Inlet and outlet water nitrate concentration and nitrate removal rate.The water inlet nitric nitrogen is approximately 15mgNO ₃ ^--N/L, the water outlet nitric nitrogen is down to 1mg/L gradually from 10mg/L, makes nitrate removal rate 30% to the subordinate phase later stage from the beginning bring up to and surpasses 90%.As mentioned above, 60 days reactors of beginning are to process synthetic wastewater, finish since the 60th day to subordinate phase, and reactor utilizes the water running that goes out that contains sulfide and vitriol of sulfate reduction device.Sulfide is oxidized to vitriol by nitrate.Figure 18 b has showed the total organic carbon (TOC) of water outlet.By Figure 18 b, can be found out, in this test, the total organic carbon of Inlet and outlet water is substantially constant, illustrates that this anti-nitration reaction is autotrophy rather than heterotrophism.

At the 65th day from reactor, gathering mud sample to carry out microscopical analysis and size distribution analysis.Figure 19 is a photo of showing the 65th day mud granule form of autotrophic denitrification reactor.Figure 20 describes autotrophic denitrification reactor mud granule size distribution.As shown in the chart, mean diameter is about 0.5mm. to the granule sludge data

The operation of example 7-heterotrophism oxidation SANI technique

Figure 21 has showed traditional biological denitrogenation and the operational scheme of producing the reuse water facility.The application of heterotrophism oxidation SANI technique can illustrate by engineering calculation.That is considering at present is one and had not only needed to provide biological denitrificaion to meet that water outlet requires but also needs provide 1/3 processing water as the reused water processing factory of reuse water to irrigate be used to cleaning street and automobile and view.Sewage treatment process comprises that primary clarifier, biological carbon and nitrogen removal process, second pond, mud are concentrated, sludge digestion, sludge dewatering and sludge incineration.Followed by the equipment of producing in addition reuse water, comprise and filtering and disinfection unit.

Figure 22 is a complete heterotrophism oxidation SANI process flow sheet.Owing to rinsing street and automobile and view, irrigate and do not need denitrogenation, can exempt denitrification process in the reusing sewage tributary.SANI process using upflow sludge blanket as sulfate reduction device and bacteria bed as Autotrophic nitrification and denitrification reactor.Because SANI technique does not need settling tank, therefore can reduce by 2/3 preliminary sedimentation tank and second pond volume.But perhaps needing to install a water pump comes extracting seawater to provide SANI technique required vitriol.

The COD that supposes water inlet is 400mg/L, all can be oxidized by the reduction of vitriol for guaranteeing all organic carbons, need to add 600mg/L SO toward sewage ₄ ^2-.According to the salinity of seawater, seawater approximately contains 2600mg SO ₄ ^2-/ L.Therefore, the amount of the required seawater added is approximately 0.25m ³/ m ³Treatment sewage.This is equivalent to increase by 1/4 total flux and enters system, but this or far below the standard peak value of sewage work, so belong to the acceptable scope.The hydraulic losses of supposing the water inlet position from the seashore extracting seawater to sewage work is 15m, every extraction 1m ³The energy consumption of seawater will reach 0.06kWh.Due to every processing 1m ³Sewage only needs 0.25m ³Seawater, therefore every processing 1m ³The large appointment of sewage consumes the 0.015kWh energy.

Due to sludge dewatering and a large amount of energy of burning consumption, and SANI technique has saved sludge treatment and burning process, with the traditional biological denitrification process, compares and can save 1/3 energy and reduce by 1/3 greenhouse gas emission.Therefore with the traditional activated sludge process denitrification process, compare the every processing of SANI technique 1m ³Sewage is equivalent to save about 0.15kWh energy, and this is with heterotrophism oxidation SANI art breading 1m ³During sewage ten of the energy consumption of extracting seawater times.

Generally speaking, adopt heterotrophism oxidation SANI technique can save 2/3 preliminary sedimentation tank and second pond, replace 1/3 biological denitrification process by more simple biological de-carbon process, and can save most sludge treatment and disposal facility.Can replace by the SANI technology generations traditional denitrification process of 2/3 simultaneously, provide seawater and only need increase a pumping system.According to "ball-park" estimate, can save like this 50% cost and reduce approximately 30% energy consumption and greenhouse gas emission.

Example 8-simplifies the operation of version heterotrophism oxidation SANI technique

Figure 23 simplifies version heterotrophism oxidation SANI process flow sheet.Heterotrophism oxidation SANI system is formed by traditional biological sewage disposal and reuse facility and a revision SANI process combination.For the first tributary, as heterotrophism oxidation of coal, two-stage precipitation and reused water processing facility, be the sewage disposal of standard and the design of reuse, so there is no need, do independent test and prove its suitability.For the second tributary, it utilizes the SANI technique of revision to carry out the elementary and secondary mud in degradation of sewage and the first tributary.As shown in example 1, SANI technique has successfully been degraded and has been comprised the raw waste water of preliminary sludge.Yet whether secondary mud can effectively be degraded and need further to confirm at the sulfate reduction device.In case secondary mud is degraded in the sulfate reduction device, at the autotrophy oxidation stage, again being oxidation of the sulfide into vitriol will not be a problem.

In order to test the feasibility of heterotrophism oxidation SANI technique, experiment has used a upflowing sulfate reduction granular sludge bed reactor with secondary mud and the raw waste water of degrading simultaneously.Under this layout, the diameter of testing upflowing sulphur reduction granular sludge bed reactor used is 8.8cm, high 50cm, cumulative volume 3L, effective volume 2.85L.Reactor is first at HRT12 hour, and under the condition that internal reflux is 5 times, operation is 14 days, carries out subsequently the water sample analysis of continuous three days.

In order to simulate above-mentioned degradation process, the preparation of water inlet has mixed the stock solution of table three and has picked up from a local secondary mud of processing the B-grade sewage treatment plant of saline sewage, so that total COD of water inlet reaches about 500mg/L, 70% COD(350mg COD/L wherein) from storing solution, remaining 30% COD(150mg COD/L, be 100mg VSS/L) from secondary mud, and the seawater of usining from salt water flushing system provides vitriol as electron carrier.

Detect index and comprise Inlet and outlet water solvability COD and particle state COD, VSS, vitriol, VFA, PH, basicity and water outlet sulfide.The average water quality of Inlet and outlet water is as listed as table six.

Table six sulphur reduction granular sludge bed reactor is processed artificial synthetic wastewater effect

Parameter	Water inlet	Water outlet	Remove
				Total COD (mg/L)	502	169	333(66%)
Solvability COD (mg/L)	250	98	152(61%)
				Particle COD (mg/L)	252	70	182(72%)
TSS(mg/L)	351	107	244(71%)
				VSS(mg/L)	252	59	163(77%)
Basicity (mgCaCO 3/L)	165	699	?
				Vitriol (mgSO 4 2--S/L)	293	127	166(57%)
Sulfide (mgS 2--S/L)	?	142	?

The total removal amount of COD is 333mg/L(or 66%) simultaneously the VSS clearance reach 77%.The total sulphur concentration of water outlet is 269mg/L, means that sulphur budget reaches 92%.Due to 1mg SO ₄ ^2--S changes into 1mg S ^2--S equals to consume 2mg COD, and about 284-332mgCOD is removed in the sulphur budget explanation, is equivalent to the COD balance of overall 92%-100%.In this numeric ratio reactor, the removal of solvability COD is high a lot.This shows that secondary mud is effectively degraded, rather than accumulates in reactor.This is tested, and sufficient proof is disposed of sewage with the sulfate reduction device and the feasibility of secondary active sludge, also proves simultaneously the possibility of application heterotrophism oxidation SANI art breading sanitary sewage.

Be understandable that, in principle of the present invention with in as claims limited range of enclosing, those skilled in the art can separately do change to details, material, step and layout, and these details, material, step and layout described herein and that illustrate are used to the essence of explain principals.

Claims (34)

1. a processing contains the biological sewage treatment method of the water inlet of organic carbon, and the method comprises:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to sulfide;

Utilize oxygen that ammonia oxidation is become to nitrate; And

Utilize nitrate that described sulfide is oxidized to vitriol, simultaneously described nitrate reduction is become to nitrogen.

2. method claimed in claim 1 further comprises:

Utilize sulphur or sulphur compound, by the sulphur compound reducing bacteria, described organic carbon is changed into to carbonic acid gas;

Utilize the autotrophic denitrification sulfur-oxidizing bacteria, by nitrate, described sulfide is oxidized to vitriol; And

By Autotrophic nitrification, described ammonia oxidation is become to nitrate.

3. the described method of claim 1 or 2, wherein said sulphur or sulphur compound comprise the material that is selected from the group that sulphite, thiosulphate and elemental sulfur form.

4. a processing contains the biological sewage treatment method of the water inlet of organic carbon, and the method comprises:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to sulfide; And

Utilize oxygen that described sulfide is oxidized to vitriol.

5. method claimed in claim 4, wherein said sulphur or sulphur compound comprise the material that is selected from the group that vitriol, sulphite, thiosulphate and elemental sulfur form.

6. claim 4 or 5 described biological effluent treatment methods further comprise:

Utilize described sulphur or sulphur compound, by the sulphur compound reducing bacteria, described organic carbon is oxidized to carbonic acid gas;

Utilize oxygen, by the autotrophy sulfur-oxidizing bacteria, described sulfide is oxidized to vitriol.

7. a processing contains the biological sewage treatment method of the water inlet of organic carbon, and the method comprises:

In the upflowing granular sludge bed reactor, utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to sulfide; And

Utilize oxygen or nitrate that described sulfide is oxidized to vitriol.

8. method claimed in claim 7, wherein said sulphur or sulphur compound comprise the material that is selected from the group that vitriol, sulphite, thiosulphate and elemental sulfur form.

9. the described biological sewage treatment method of claim 7 or 8, wherein said upflow sludge bed reactor comprise that further internal reflux pump and flow restriction device increase the turbulent flow in reactor.

10. a processing contains the biological sewage treatment method of the water inlet of organic carbon, and the method comprises:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to sulfide; And

In the upflowing granular sludge bed reactor, utilize oxygen or nitrate, by the oxidation of autotrophy sulphur, described sulfide is oxidized to vitriol.

11. method claimed in claim 10, wherein said sulphur or sulphur compound comprise the material that is selected from the group that vitriol, sulphite, thiosulphate and elemental sulfur form.

12. in claim 4 to 11, the described method of any one, further comprise and utilize nitrobacteria that ammonia oxidation is become to nitrate.

13. the described method of any one in claim 4 to 12, further comprise and used the water inlet that contains a large amount of salinities.

14. a processing contains the biological sewage treatment method of the water inlet of organic carbon, the method comprises:

Provide parallel tributary for biological treatment, in conjunction with as follows:

In the first tributary, utilize oxygen or nitrate that described organic carbon is oxidized to carbonic acid gas; And

In the second tributary, utilize sulphur or sulphur compound, by the sulphur reducing bacteria, described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to sulfide, this sulfide is oxidized to vitriol by oxygen or nitrate subsequently.

15. the described method of claim 14, further comprise and utilize additional process steps to realize the processing effluent reuse in described the first tributary, wherein this additional process steps is selected from the group of filtering and sterilizing and forming.

16. the described method of claims 14 or 15 further comprises:

Collect the mud that described the first tributary produces; And

In described the second tributary, described mud and water inlet are mixed to co-treatment.

17. the described method of claim 14, wherein said sulphur or sulphur compound comprise the material that is selected from the group that vitriol, sulphite, thiosulphate and elemental sulfur form.

18. the described method of any one in claim 14 to 17, further be included in the one or both in described the first tributary and described the second tributary, utilizes nitrification that ammonia oxidation is become to nitrate.

19. the described method of any one in claim 14 to 18, further comprise and used the water inlet that contains a large amount of salinities.

20. a processing contains the biological sewage treatment plant of the water inlet of organic carbon, comprising:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, and simultaneously described sulphur or sulphur compound are reduced into to the reactor of sulfide;

Be used for described sulfide is oxidized to vitriol and simultaneously nitrate reduction is become to the reactor of nitrogen; And

Be used for ammonia oxidation is become the reactor of nitrate.

21. a processing contains the biological sewage treatment plant of the water inlet of organic carbon, comprising:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to the approach of sulfide;

Utilize nitrate that described sulfide is oxidized to vitriol, simultaneously described nitrate reduction is become to the approach of nitrogen; And

Ammonia oxidation is become to the approach of nitrate.

22. claim 20 or 21 described biological sewage treatment plants, wherein said sulphur or sulphur compound comprise the material that is selected from the group that sulphite, thiosulphate and elemental sulfur form.

23. a processing contains the biological sewage treatment plant of the water inlet of organic carbon, comprising:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, and simultaneously described sulphur or sulphur compound are reduced into to the reactor of sulfide; And

Utilize oxygen described sulfide to be oxidized to the reactor of vitriol.

24. a processing contains the biological sewage treatment plant of the water inlet of organic carbon, comprising:

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to the approach of sulfide; And

Utilize oxygen described sulfide to be oxidized to the approach of vitriol.

25. claim 23 or 24 described biological sewage treatment plants, wherein said sulphur or sulphur compound comprise the material that is selected from the group that vitriol, sulphite, thiosulphate and elemental sulfur form.

26. in claim 23 to 25, the described biological sewage of any one treatment plant, further comprise ammonia oxidation become to nitrate.

27. in claim 23 to 26, the described biological sewage of any one treatment plant, further comprise and used the water inlet that contains a large amount of salinities.

28. a processing contains the biological sewage treatment plant of the water inlet of organic carbon, comprising:

Utilize oxygen or nitrate described organic carbon to be oxidized to the reactor of carbonic acid gas;

Utilize sulphur or sulphur compound that organic carbon is oxidized to carbonic acid gas, and simultaneously described sulphur or sulphur compound are reduced into to the reactor of sulfide; And

Utilize oxygen or nitrate described sulfide to be oxidized to the reactor of vitriol.

29. a processing contains the biological sewage treatment plant of the water inlet of organic carbon, comprising:

Utilize oxygen or nitrate described organic carbon to be oxidized to the approach of carbonic acid gas;

Utilize sulphur or sulphur compound that described organic carbon is oxidized to carbonic acid gas, simultaneously described sulphur or sulphur compound are reduced into to the approach of sulfide; And

Utilize oxygen or nitrate described sulfide to be oxidized to the approach of vitriol.

30. claim 28 or 29 described biological sewage treatment plants, further comprise mud and the water inlet sewage combination treatment of utilizing sulphur or sulphur compound will come from oxygen or nitrate oxidation organic carbon process, so that described organic carbon is oxidized to carbonic acid gas, and simultaneously described sulphur or sulphur compound are reduced into to sulfide.

31. the described biological sewage of any one treatment plant in claim 28 to 30, wherein said sulphur or sulphur compound comprise the material that is selected from the group that vitriol, sulphite, thiosulphate and elemental sulfur form.

32. the described biological sewage of any one treatment plant in claim 28 to 31, further comprise Sewage Reuse System, namely for through oxygen or the described organic carbon of nitrate oxidation and the processing water outlet produced, by additional process steps, realize the reuse of this processing water outlet, wherein this additional process steps is selected from the group of filtering and sterilizing and forming.

33. in claim 28 to 32, the described biological sewage of any one treatment plant, further comprise the facility that ammonia oxidation is become to nitrate.

34. the described biological sewage of any one treatment plant in claim 28 to 33, further comprise the facility that uses the water inlet that contains a large amount of salinities.

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